High purity mortar suitable for bonding refractory brick

ABSTRACT

A high purity mortor suitable for bonding refractory brick is disclosed. The mortar, which is resistant to attack by molten aluminum, comprises 43 to 89 wt.% alumina aggregate, 10 to 45 wt.% calcium aluminate cement, 0.5 to 10 wt.% zinc borosilicate and 0.1 to 1.5 wt.% boric acid.

BACKGROUND OF THE INVENTION

This invention relates to high purity cement and more particularly itrelates to a high purity cement suitable for bonding refractory brick.

Because of the growing awareness of the limitation on natural resources,particularly energy resources, considerable effort has been expended toproduce alternate sources. One such source which is considered to haveexceptional long term potential to fulfill this need is the energy froma fusion nuclear reactor. However, because of the need to isolate orconfine the radioactive media involved, considerable investigation isunderway to develop materials for the reactor which will notsubsequently present disposal problems. For example, if extreme purityaluminum were used in the reactor, the radioactivity of such materialwould be reduced by a factor of a million a few weeks after shutdown,provided the purity of the aluminum was sufficiently high. Bycomparison, if stainless steel were used for the same application, thisreduction would take about 1000 years, obviously presenting difficultproblems in disposing of such materials.

Another energy related field where extreme purity aluminum can be usedto great advantage is stabilization of superconductors. In thisapplication, the electrical energy is transferred at cryogenictemperatures, e.g. 4° K., where the electrical resistance is very low.The use of extreme purity aluminum as a stabilizer is preferred in thisapplication because of its very low resistivity, i.e. high conductivityat such low temperatures.

For example, aluminum having a purity of 99.9 wt.% would have anelectrial conductivity factor at 4° K. of 20 times that of its roomtemperature value while a 99.999 wt.% aluminum would have acorresponding increase in conductivity of at least 1000 times and a99.999 wt.% aluminum would have a conductivity factor at 4° K. of 5000times its room temperature value. Thus, the total purity of the aluminumgives a reasonable indication of the conductivity at 4° K. However, theconcentration of certain critical impurities is more important. Thesecritical impurities include titanium, vanadium, zirconium, chromium,manganese and iron. For example, the effect of chromium on lowtemperature conductivity is 20 times greater per ppm than copper--arelatively innocuous impurity as far as superconducting applications areconcerned. Unfortunately, none of the prior art processes is effectivein completely removing all of these critical impurities at reasonablecosts.

For many years, purified aluminum was produced in an electrolytic cellhaving three liquid layers--two molten aluminum layers separated by asalt or electrolyte layer. The bottom or lower layer in the cell is theimpure or aluminum-copper alloy layer and formed the anode of the celland was purified by electrolytically transferring molten aluminumthrough the intermediate salt layer to the higher purity molten aluminumlayer or cathode. Such cells, in various forms, are described in HoopesU.S. Pat. No. 1,534,320; Hoopes U.S. Pat. No. 1,535,458; Hoopes U.S.Pat. No. 1,562,090 and Hulin U.S. Pat. No. 1,782,616, for example. Thiselectrolytic cell, known to those skilled in the art as the Hoopes cell,is effective in reducing impurities such as manganese, chromium,titanium, vanadium, zirconium and gallium to a very low level. However,such a cell is less effective in lowering the concentration ofimpurities such as silicon, iron, copper and the like. That is, afterpassing aluminum to be purified through a Hoopes cell, significantamounts of silicon, iron and copper can be found in the high puritycathode layer, although at much lower concentrations than in the anodelayer.

The prior art also discloses that high purity aluminum can be producedby several other methods; however, all of these methods takenindividually can have serious drawbacks, especially when it is desiredto produce large quantities of extreme purity aluminum at economicallyattractive costs. For example, zone refining, which can produce extremepurity aluminum, has the disadvantage that it can be difficult to scaleto production quantities.

It is also known that certain impurities can be removed by adding boronto aluminum in the molten condition, thereby forming a boron-containingcompound or complex having a higher density than the aluminum, resultingin the compound precipitating out. This process of purifying aluminum istaught by Stroup in U.S. Pat. No. 3,198,625 and described in an articleby Russell et al entitled "A New Process to Produce High-PurityAluminum" at pp. 1630 to 1633 of Vol. 239, Transaction of theMetallurgical Society of AIME (October 1967). However, as noted in thepatent, while this process is particularly effective in removingtitanium, vanadium, zirconium, and to a lesser degree chromium, it hassubstantially no effect on the removal of other common impurities suchas iron, silicon, copper and the like.

Another method in the prior art used for the purification of aluminum isreferred to as preferential or fractional crystallization. Suchcrystallization methods are disclosed by Jarrett et al in U.S. Pat. No.3,211,547 and by Jacobs in U.S. Pat. No. 3,303,019 (both patentsincluded herein by reference) and in the aforementioned Russell et alarticle. However, while the methods disclosed in these publications canresult in fractions of very high purity aluminum, there also results, asdisclosed by Jarrett, a fraction of relatively low economic value and atleast one intermediate fraction, in respect to aluminum which is notwidely variant from the starting material. Furthermore, this processdoes not remove elements such as titanium, zirconium, vanadium,manganese and chromium.

While each of the foregoing prior art processes is effective for theremoval of certain impurities, none of the processes individually removeall of the undesirable impurities which should be removed for certainapplications of extreme purity aluminum such as in the field ofsuperconductors as previously discussed. Furthermore, each of theprocesses suffers economically--the fractional crystallization becauseof the low yield of high purity aluminum per kilogram of aluminum whichmust be heated to its melting point to permit such separations and theelectrolytic purification because it does not effectively remove allimpurities to a sufficiently low level.

The present invention solves the problems such as described in the priorart involving purification of aluminum by providing a process whichproduces extreme purity aluminum in an economical manner in largeproduction quantities and in which process, for every pound of impurealuminum beneficiated, almost one pound of extreme purity aluminum isobtained. The cost of extreme purity aluminum produced in accordancewith the present invention is quite low compared to conventionalpractices.

SUMMARY OF THE INVENTION

An object of the present invention to provide high purity mortar for theeconomical production of extreme purity aluminum.

Another object of the present invention is to provide a high puritymortar resistant to attack from molten aluminum.

In accordance with these objects, a high purity mortar suitable forbonding refractory brick is provided. The mortar which is resistant toattack by molten aluminum comprises 43 to 89 wt.% alumina, 10 to 45 wt.%calcium aluminate cement, 0.5 to 10 wt.% zinc borosilicate and 0.1 to1.5 wt.% boric acid.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a flow diagram of the process of the invention.

FIG. 2 is an elevational view of a three-layer electrolytic cell of theinvention.

FIG. 3 illustrates schematically a sectional elevation of a fractionalcrystallization furnace for use in the process of the present invention.

FIG. 4 is a flow diagram illustrating a preferred embodiment of theinvention.

FIG. 5 is a flow diagram illustrating another preferred embodiment ofthe invention.

FIG. 6 is a graph showing the concentration factor of silicon in impurealuminum plotted against the percent of charge removed.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

Referring more particularly to FIG. 1, it will be seen that inaccordance with certain aspects of the present invention, aluminum to beselectively purified of impurities is provided in molten form as theanode of a three-layer electrolytic cell referred to by those skilled inthe art as a Hoopes cell. This molten aluminum anode layer constitutesthe lower or bottom layer in the cell, which layer is separated from amolten aluminum cathode layer by a molten salt layer normally referredto as the electrolyte. The molten aluminum cathode layer, which byoperation of the cell to electrolytically transport molten aluminumthrough the electrolyte, constitutes aluminum in which selectedimpurities have been substantially lowered.

To further describe the broad aspects of the invention, aluminum fromthe molten cathode is next subjected to a further purification stepreferred to as preferential or fractional crystallization. In thefractional crystallization process, aluminum-rich crystals are formed bycontrolled freezing or solidification of high purity aluminum. That is,molten aluminum low in impurity content has a higher freezingtemperature than aluminum with a higher impurity level, often referredto as the mother liquor. After crystallization of the pure aluminum, themother liquor, with its higher impurity content, is drained off leavingbehind aluminum crystals or a fraction of aluminum very low in impuritycontent. The mother liquor removed can constitute half or more of thetotal aluminum products from the fractional crystallization step. Thisportion of the mother liquor is normally, in the conventional operationof the fractional crystallization process, of lower value since it has ahigher level of impurity and conventionally is not further used forpurification purposes. That is, this portion, drained from the aluminumrich crystals, has a much higher impurity level than the startingmaterial in the crystallization process and can be more difficult topurify than the starting material referred to above.

In accordance with one embodiment of the present invention, the highimpurity portion or the mother liquor is recycled through thethree-layer electrolytic cell where impurities that tend to concentratein the fractional crystallization step can be reduced once again to alevel suitable for economical processing in the fractionalcrystallization process, as can be seen in FIG. 1. Thus, byrecirculating the high impurity fraction, substantially all, typically90 to 95%, of the impure aluminum provided in the molten aluminum anodelayer can be recovered as extreme purity aluminum. That is,substantially all the impure aluminum provided or melted into the anodeof the system is recovered either as high purity aluminum or as recycledmolten metal to be refed into the anode layer. It will be appreciatedthat recirculating the impure molten aluminum mother liquor results insubstantial savings, for example, in the energy required to remeltprimary aluminum or the like containing impurities. Also, there is theadditional savings in the inventory of impure or primary aluminumrequired to produce high purity aluminum.

Because of the selective removal of certain impurities in the system ofthe present invention, many aluminum sources can be used withoutpresenting problems to the system. However, the more suitable sourcesinclude primary aluminum which typically consists of 99.6 wt.% aluminum,the remainder consisting essentially of impurities with respect to thehigh purity aluminum obtainable by the present system. It will beunderstood that in some cases the primary aluminum can be as high as99.9 wt.% which obviously is beneficial in the use of this invention.The impurities referred to include typically iron, silicon, titanium,vanadium, manganese, magnesium, gallium, copper, sodium, barium,zirconium, chromium, nickel and zinc. It will be seen hereinbelow thatthese impurities are readily removed to provide large commercialquantities of extreme purity aluminum product, that is, aluminum havinga purity of at least 99.995 wt.%.

The three-layer electrolytic cell referred to is an important aspect ofthe present invention. A preferred cell structure for producing purifiedaluminum in accordance with the system of the present invention isillustrated in FIG. 2. The cell illustrated includes an outer insulatingrefractory wall 20, a carbon or graphite floor or bottom portion 22 anda special lining material 24 which aids in producing purified aluminum.The cell has a charging well 26 through which primary aluminum, forexample, is added to molten anode 28. Wall 30 separates the impuremolten aluminum in the forewell from electrolytic layer 32 and thepurified aluminum layer 34. A lid or cover 36 over the cell reduces aircontact and prevents skim formation on the cathode layer 34 of purifiedaluminum.

The special lining material 24 is an important aspect of the cell. Thelining material 24 comprises high purity alumina bricks bonded with aparticular mortar. The high purity alumina bricks consist of at least 90wt.% Al₂ O₃, preferably 92 to 99 wt.%. The mortar typically consistsessentially of 64.5 wt.% of 99 wt.% purity tabular alumina (-48 mesh);33 wt.% calcium aluminate cement such as sold by Alcoa as CA-25containing 18 wt.% CaO, 79 wt.% Al₂ O₃, 1 wt.% impurities and 2 wt.%LOI; 2 wt.% zinc borosilicate; and 0.5 wt.% H₃ BO₃. This type liner, aswell as being electrically nonconductive, is thermally insulating andresistant to attack by molten aluminum and molten salts at operatingtemperatures. Thus, the cathode layer 34 of purified aluminum is notcontaminated by liner decomposition. In the prior art, such liner wastypically made from magnesium oxide which was less pure and alsoresulted in increased magnesium in the purified cathode layer.

With respect to the mortar, alumina therein can range from about 43 to89 wt.%, with a preferred range being about 54 to 74 wt.%. Also, thecalcium aluminate cement can range from 10 to 45 wt.%, with a preferredrange being about 25 to 40 wt.%. Normally, the level of impurities, e.g.silica and iron oxide, in the calcium aluminate cement should not begreater than about 1.5 wt.%, particularly if the use is in aluminumpurification. Calcium aluminate cement having about this level ofimpurity and having about 71 wt.% Al₂ O₃ and 27 wt.% CaO can be obtainedfrom Denki Kagaku Kogyo KK, Sanshin Building 4-1, Yuraku-cho 1-chome,Chiyoda-ku, Tokyo 100, Japan, and is referred to as Denka cement.However, in certain instances where purity is of lesser importance,higher levels of impurities can be tolerated without adversely affectingthe integrity of the bond. For example, the level of impurity in thecalcium aluminate cement can be as high as 7.5 wt.% in certaininstances. Calcium aluminate cement having about this higher level ofimpurity and containing about 53 wt.% Al₂ O₃ and about 35 wt.% CaO maybe obtained from Universal Atlas Cement, Division of U.S. SteelCorporation, 600 Grant Street, Pittsburgh, Pa. 15230 and is referred toas Refcon.

With respect to the size of alumina aggregate, such as tabular,sintered, fused and/or ground calcined alumina, typically it would notbe greater than 14 mesh (Tyler Series) with a preferred size being about-48 mesh (Tyler Series). Refractory mortar joints for which the mortarof the invention has application are normally very thin, typically notexceeding 1/8 inch. In such application, normally, the coarsestaggregate size in such mortar should be no more than about one-third thedesired mortar joint thickness.

As noted earlier, the anode and cathode comprise molten aluminum layersseparated by a molten salt or electrolytic layer. With respect to theanode, it should comprise about 20 to 30 wt.% copper, the remainderaluminum and impurities, thus providing a density of about 2.8 to 3.1grams per cubic cm at 800° C., a density which will be greater than thatof the electrolyte at the operating temperatures of the cell, i.e. fromabout 750° to 850° C.

With respect to the electrolyte, typically it is a molten mixturecontaining from 18 to 23 wt.% sodium fluoride, 36 to 48 wt.% aluminumfluoride, 18 to 27 wt.% barium fluoride and 14 to 20 wt.% calciumfluoride. Strontium fluoride may be substituted for the barium fluorideif desired. The addition of barium fluoride to the electrolyte providesa density somewhat greater than the purified aluminum, i.e. about 2.5 to2.7 grams per cubic cm at 800° C. The pure aluminum has a density ofabout 2.33 grams per cubic cm at 800° C. Other mixtures of alkali andalkaline halogens can also be used in the electrolyte layer, as is wellknown to those skilled in the art, such as mixed fluoride-chloridesystems. The density of the particular mixture must, however, be greaterthan that of pure aluminum (99.995 wt.% or higher) at the operatingtemperature of the cell.

With respect to the depth of the molten layers, the anode layer can havea depth in the range of 39.1 to 63.5 cm (15 to 25 in.); the electrolytelayer, a thickness of at least 10.2 cm (4 in.); and preferably notgreater than 20.3 cm (8 in.); and the cathode layer a depth in the rangeof about 7.6 to 22.9 cm (3 to 9 in.).

In a preferred embodiment of the cell, electrode 38 is mounted on bar 40which projects through cover 36. Preferably, bar 40 is coated with arefractory, such as an alumina base refractory available from PlibricoCompany, Chicago, Ill., under the designation Plistix 900, to preventflaking of the collector metal and is further provided with a hightemperature rope seal 42, e.g. asbestos rope, to prevent air or othersuch gases from entering or leaving the cell, thus minimizing burning ofthe electrodes and formation of skim. In a further preferred embodiment,sealed cover 36 allows for the injection of inert or reducing gases intospace 44 which further ensures against oxidation of the electrodes, bathand cathode metal. Such gases include helium, neon, argon, krypton,xenon, along with nitrogen, carbon dioxide and mixtures thereof.

It has been found that by sealing the unit and providing an inertatmosphere that graphite cathodes will last at least one year. Becauseair burning is minimized, contamination of the top metal from cathodeimpurities is greatly reduced if not completely eliminated. It is alsoeconomically feasible to use high purity graphite in this application.

An important feature of the present invention is electrode 38 andplacement or location of the bottom side 39 thereof with respect toelectrolyte 32. Preferably, bottom side 39 is immersed in theelectrolyte, and further preferably, the distance between the top 46 ofanode layer 28 and bottom side 39 of electrode 38 is in the range of 40to 60% of the thickness of electrolyte layer 32. Having electrode 38arranged to separate the cathode and the anode layers in this wayreduces the electrical energy required to operate the cell by up toabout 25%. The cell is operated, preferably at a current density of0.388 to 0.465 amperes per square centimeter (2.4 to 3.0 amps/inch²).

As will be seen by reference to FIG. 1, molten aluminum forming thecathode of the electrolytic cell is removed, typically on a periodicbasis, during operation of the cell and thereafter subjected to furtherpurification by fractional crystallization. Typically, this latter typeof purification removes eutectic impurities. By eutectic impurities ismeant metallic impurities which, when present in aluminum in sufficientamount, form in the solidified metal a structure which contains aluminumand which has a lower melting point than pure aluminum. Typical of theseimpurities is iron and silicon.

According to the system of the present invention, the partially purifiedaluminum is further purified in a fractional crystallization step whichcomprises cooling molten aluminum to a temperature just below themelting point of the pure aluminum, or at the point where the purealuminum solidifies. The impure liquid can then be removed and thenreturned to the electrolytic cell, if desired. For purposes of thefractional crystallization step, it is preferred in the practice of thepresent invention to place the molten aluminum from the cathode of theelectrolytic cell in a container so that the body of molten aluminum hasa free or unconfined surface. The temperature of the walls of thecontainer are controlled by insulation or by heating so that little orno heat flows outwardly from the molten aluminum body. Heat is withdrawnor removed at the unconfined surface to obtain solidification of themolten aluminum which brings about fractional crystallization of thepure aluminum in a zone at and immediately under the molten metalunconfined surface. Freezing of the molten metal at the walls of thecontainer should be prevented if possible, or, if some freezing doesoccur, it should not constitute more than 10% of the molten body. Moltenaluminum which solidifies at the container wall should not be permittedto contaminate crystallization occurring at the zone at and beneath theunconfined surface.

Referring now to FIG. 3, there is shown a container 60 for thefractional crystallization process having an insulating wall 62 whichmay be heated if desired. The container, preferably, has a layer 64comprising powdered alumina which provides a barrier to molten aluminumwhich may escape through inside wall 66. Wall 66 should comprise amaterial which will not act as a source of contaminant to the moltenaluminum 74. Wall 66 is preferably constructed from high purityalumina-based refractories, i.e. at least 90 wt.% and preferably 92 to99 wt.% alumina. One such refractory may be obtained from NortonCompany, Worcester, Mass., under the designation Alundum VA-112. Thismaterial is provided in wall 66 in powdered form, compacted, and thensintered thereby giving it rigidity. This forms a monolithic liningwhich is less likely to be penetrated by molten aluminum and thus ismore suitable for use with a bottom heating system as will be describedbelow. For example, material balance checks show a recovery of 99.7 wt.%of the initial charge indicating little or no penetration of the lining.

The use of a high purity alumina lining such as Alundum provides verylittle contamination. For example, the maximum contamination by iron orsilicon of the total charge is usually not greater than 2 ppm iron and 3ppm silicon and often is less than 1 ppm iron and silicon; some of thismay be attributable to contamination from taphole plugs or the like.Furthermore, sidewall freezing which is also to be avoided, for highpurity production, is less of a problem using such a lining than priorart uses of materials such as silicon carbide, or the like.

Molten aluminum constituting the cathode layer 34 in the aforementionedHoopes cell is impure in the sense that it contains unwanted eutecticimpurities. To remove these impurities by fractional crystallization,heat is removed from this molten aluminum (sometimes referred to as thefreeze cycle) at such a rate so as to form and maintain aluminum-richcrystals in zone 70, as shown in FIG. 3. Aluminum-rich crystals thusformed settle by gravity into zone 72 and, after a predetermined amountof fractional crystallization takes place, the remaining impure moltenaluminum, typically concentrated in the upper part of the unit and highin eutectic impurity, can be separated from the aluminum-rich or highpurity aluminum by drainage through taphole 76. During the freeze cycle,it is preferred to facilitate the crystal settling process by action oftamper 78 which breaks up massive crystal formations and compacts thecrystals in zone 72, as described in the aforementioned Jarrett et alpatent. After removal of the impure mother liquor via taphole 76, thecontainer can be heated to remelt the pure aluminum crystals which arethen removed via lower taphole 80.

In accordance with a preferred aspect of the invention, crystals arepacked or compacted during the freeze cycle to squeeze out impure liquidfrom between the crystals located generally in the bottom region 72 ofthe vessel. Impure liquid having been more or less displaced from area72 of the unit is removed via upper taphole 76, thus eliminating passingsuch liquid through the high purity lower region of the crystal bedlocated generally in bottom 72 of the unit. During the freezing andcompacting cycle, it has been discovered that a larger fraction ofhigher purity aluminum can be obtained by heating the bottom of the unitduring the freeze cycle. This heat may be supplied by external inductioncoils or by resistance wires or globars contained in tubes in theAlundum lining. Silicon carbide type globars, available from theaforementioned Norton Company, may be used. As noted earlier, the use ofa monolithic lining which prevents penetration of molten aluminumpermits the use of such heating means embedded in the lining. For addedprotection, each globar 110 may be inserted in a tube of material 100,for example mullite, which is nonconducting and not penetrable by moltenaluminum. While the heating means has been shown in the bottom of layer66 (FIG. 3), it will be understood that additional heating elements maybe placed in the sides with beneficial effect.

Heating at or near the bottom of the unit during the freeze cycle, i.e.while heat is being removed at or near the surface, permits remelting ofa portion of the crystals located near the bottom of the unit. Thismelted portion rises or is displaced up through the crystal bed carryingwith it impure liquid remaining therein. The rising or displacement ofthe melted portion up through the crystals is believed to be facilitatedby crystals tending to displace the melted portion at or near the bottomof the unit since crystal density is greater than that of the liquidphase or melted portion. Further, bottom heating is very beneficialduring the packing or compacting process in that a melted portion isprovided which can be squeezed up through the crystal bed carrying withit impurities remaining between the crystals or adhering thereto. Bottomheating is also advantageous in that it can prevent freezing of theliquid phase on the bottom entrapping impurities therein which can havean adverse effect on the purity level when all of the crystals areeventually remelted for purposes of removal through lower taphole 80.

It will be understood that normally bottom heating should be carefullycontrolled during the freeze cycle to prevent excessive remelting.Typically, heating at or adjacent the bottom during the freeze cycleshould be controlled so as to introduce heat at a rate of substantiallynot less than 1 Kw/ft² of heating area, depending to a certain extent onheat removal at or near the surface for crystallization purposes anddepending on insulative values of the walls. A typical heating range atthe bottom of the unit is 0.5 to 3.0 Kw/ft². It will be noted thatnormally the bottom heating rate is controlled so as to be a fraction ofthe rate at which the heat is removed. It has been found that typicallybest results are achieved when the remelt rate at or near the bottom ofthe unit is controlled so as to be in the range of about 5 to 25% of thecrystallization or freeze rate. However, there can be instances whenthese rates may be higher or lower depending somewhat on the pressureused in packing and density of the crystal bed.

The advantages of having controlled heating adjacent the bottom of thevessel for purposes of controlled remelting of crystals are clearlyillustrated by reference to FIG. 6 which shows the level of impurity forsilicon, for example, which may be achieved with or without bottomheating. That is, FIG. 6 shows the concentration factor (ratio ofimpurity concentration in a sample to the impurity concentration in thecharge) of silicon plotted against the amount of aluminum removed fromthe crystallization unit. For example, if the initial concentration ofsilicon in the unit is 360 ppm and its concentration factor (CF) is 1,it will be noted from FIG. 6 that by utilizing bottom heating theconcentration of silicon versus the amount of aluminum removed is high(3.7) compared to the concentration of silicon using a conventionalfreeze cycle. The high concentration factor is significant in that,first, a greater amount of impurity can be removed through the uppertaphole as can be seen from FIG. 6. Secondly, only a smaller amount ofaluminum has to be removed (about 30% in the instance shown in FIG. 6)to significantly lower the impurity level. That is, from FIG. 6 it willbe seen that by the conventional freeze cycle, approximately 60 to 70%of the charge had to be removed for comparable removal of impurity.However, in the present invention as much as 60% of the charge can berecovered as high purity product. It can be seen that by using bottomheating a significant increase in the yield of purified metal can beachieved. Referring to FIG. 6 as an example, it will be noted that theyield can be doubled. It will be understood that higher concentrationfactors may be obtained by change of packing pressure and bottomheating. That is, impurities can be further concentrated therebypermitting a smaller fraction to be removed via the upper taphole,resulting in even greater yields.

While it is not clearly understood why bottom heating as well ascompacting provides such advantages with respect to yield, it has beennoted that such practice results in purity factors, for example foriron, much higher than would be theoretically explainable by binaryphase diagrams. For example, if the starting Fe content is 0.05 wt.%,the binary phase diagram shows that the highest purity material shouldcontain 0.0014 wt.% Fe corresponding to a maximum purification factor of37. Experiments have been carried out, however, using the aboveprocedure where some material has less than 0.0005 wt.% Fe even as lowas 0.0003 wt.% Fe. This extra purification seems only explainable byreplacement of the original liquid by purer liquid through the mechanismof bottom heating and packing. The crystals then equilibrate with thepurer liquid according to the theoretical partition functions. That is,it is believed that there is a solid state mass transfer phenomenathrough and from the solid crystal to a purer liquid phase surroundingthe crystal in order to equilibrate with the liquid phase.

The freeze or crystal forming cycle can be carried out over a period offrom about two to seven hours. The heating of the bottom of the unit mayextend for the same period for purposes of partially remelting some ofthe crystals near the bottom of the bed 72 (FIG. 3). It has been found,though, that bottom heating may be used only for part of the freezecycle and typically for about the last two-thirds of the freeze cycle.

As well as using bottom heating during the freeze cycle, it has beenfound that such heating is beneficial also during remelting of thecrystals for purposes of their recovery from the fractionalcrystallization unit. That is, in addition to remelting of the extremepurity product crystals by conventional surface heating, heat issupplied to the bottom of the unit in the same manner as describedabove. Utilizing bottom heating during the remelting cycle has theadvantage that it prevents the liquid phase in the high purity productfrom freezing at or near the bottom of the vessel which can interferewith purity level. Further, keeping the high purity product in moltenform facilitates opening of the lower taphole. Additionally, bottomheating reduces the period required to melt the crystal bed in the unit,greatly increasing the overall economies of the system. Typically,melting of the crystal bed requires about two to five hours.

In accordance with the practice of the present invention, moltenaluminum 74, high in eutectic impurity (mother liquor), may be returnedto the Hoopes cell, as will be seen by reference to FIG. 1. The eutecticimpurities which concentrated in the fractional crystallization step canonce again be lowered to a predetermined level in the Hoopes cell.Primary aluminum or the like and mother liquor 74 are both added to theHoopes cell so that together they are substantially commensurate inamount with that withdrawn from the cathode.

In a preferred aspect of the present invention shown in FIG. 4, themother liquor or high impurity aluminum 74 removed from the fractionalcrystallization step, denoted as Stage 1 in the drawing, is subjected toat least one additional fractional crystallization treatment in Stage Rsubstantially in the same manner as referred to with reference to thepreviously described fractional crystallization step. While this isshown in the drawing as a separate step, it should be understood thatthe same fractional crystallization apparatus may be used for more thanone step or stage of purification. As in the previous embodiment, thedowngraded cut from Stage R is returned to the Hoopes cell. However, thealuminum-rich crystals or purified cut of aluminum from Stage R isreturned to the Stage 1 fractional crystallization step where it isblended with molten aluminum or feed from the Hoopes cell. The total ofthese two amounts should be commensurate with the amount which the Stage1 fractional crystallization unit can process economically. It will beappreciated by those skilled in the art that the mother liquor returnedto the Hoopes cell may not be as impure as the original feed stock tothe cell. Likewise, the purified or aluminum rich fraction returned tothe first fractional crystallization step may not be as impure as themetal from the Hoopes cell.

It should be understood that the Hoopes cell is normally inherently morecostly to operate than the fractional crystallization unit. Thus, metalwhich must be processed in the Hoopes cell will be more expensive.Therefore, it can be seen that a minimal amount of subsequent fractionsshould be returned to be further processed in the Hoopes cell. That is,preferably more than one fractional crystallization treatment should beprovided in order to minimize the amount of material returned to theHoopes cell.

Thus, referring to FIG. 5 it will be seen that three stages offractional crystallization may be used. That is, another crystallizationstage can be used to increase the purity of the product from 99.999 to99.9999 wt.% aluminum. The initially purified aluminum from the cathodelayer of the electrolytic cell is fed to the Stage 1 fractionalcrystallizer. The purified aluminum fraction from Stage 1 is in turn fedto the Stage 2 fractional crystallization unit. Pure aluminum from theStage 2 fractional crystallization unit is then recovered as essentially99.9999 wt.% pure. The yield or recovery, i.e. upgraded fraction inStage 2 should be approximately 50% of the purified aluminum from Stage1 received into the Stage 2 fractional crystallizer. The remaining 50%(downgraded fraction) of the aluminum fed into the Stage 2 fractionalcrystallizer is returned to the Stage 1 fractional crystallizer. Theimpure or downgraded fraction from the Stage 1 crystallizer is in turnfed into the Stage R crystallizer. About 50% of the product of the StageR crystallizer is recovered as the purified or upgraded portion and isblended with the impure or downgraded cut from Stage 2 and the aluminumfrom the cathode layer of the electrolytic cell as a combined feed forthe Stage 1 fractional crystallizer. The impure mother liquor from StageR is fed back to the electrolytic cell to be introduced into the anodelayer. Thus, the aluminum from the cathode layer of the electrolyticcell is subjected to three stages of fractional crystallization beforethe impure mother liquor is returned to the anode layer of theelectrolytic cell.

With respect to the Hoopes cell referred to above in which certainimpurities were removed initially, in an alternate embodiment of theinvention the molten metal to be purified in said cell can beadditionally treated by adding boron to said molten metal substantiallyin the same manner as taught by Stroup in U.S. Pat. No. 3,198,625,incorporated herein by reference. By adding boron to the molten aluminumto be purified, at least one of the group of impurities composed oftitanium, chromium, vanadium, zirconium and scandium are substantiallyreduced by precipitation of a boron-containing compound or complexhaving normally a higher density than that of the molten aluminum. Theamount of boron introduced should normally be stoichiometrically greaterthan the amount of impurities. The molten aluminum may be treated by theaddition of boron in a separate container. However, in accordance withthe procedures of the present invention, it is preferred that thetreating of the molten aluminum with a source of boron be performed inthe Hoopes cell. That is, a source of boron may be provided in themolten aluminum alloy which constitutes the impure layer of the Hoopescell. The source of boron may be added to the forewell or charging well26 of the cell. It should be understood that small amounts of boron havelittle or no effect on the removal of other common impurities such asiron, silicon and copper and the like.

In a preferred mode of the invention, molten aluminum from the cathodeof the Hoopes cell should be treated with a carbonaceous material so asto remove magnesium or substantially lower any magnesium which may bepresent. Preferably, the carbonaceous material is of high purity.However, lower purity material can be used in certain cases where airburning is prevented with satisfactory results. The magnesium isbelieved to form magnesium carbide. The carbonaceous material may be ahigh purity graphite. Such graphite can be obtained from UltracarbonCorporation, Bayview, Michigan, under the trade name Ultra-F graphite.In the use of graphite for this purpose, it was discovered thatmagnesium can be reduced from more than 40 ppm down to less than 1 ppm.Preferably, high purity (99.99 wt.%) graphite is used. However, lowerpurity grades of graphite such as Union Carbide CS and AGSX in graphitemolds or crucibles may be used. The magnesium can be removed by castingpurified aluminum from the electrolytic cell in graphite crucibles or byremelting the final product in an electric furnace having a high puritygraphite lining followed by casting into high purity graphite molds orcrucibles. While the mechanism for removal of magnesium by this means isnot known, it has been postulated that magnesium carbide is formed orthat the carbon catalyzes magnesium oxide formation which is skimmedoff.

The process of the present invention has significant advantages overother processes for the production of extreme purity aluminum, one ofthe most important of which is substantial reduction in the cost of thehighly purified end product. It is this large reduction in cost whichcontributes to the feasibility of production of energy by fusionreaction. One feature of the system of the present invention whichcontributes to the cost reduction is the fact that substantially thesame amount of aluminum, e.g. primary aluminum, introduced to the systemcan be recovered as an end product and for all practical purposes verylittle metal is discarded, as in prior practices. Thus, it will be seenfrom the description of the present system that there is a uniquecooperation which operates to reduce production costs and wastes asmentioned with respect to the fractional crystallization. In addition tothe above, another advantage resides in the fact that large amounts ofhigh purity aluminum, e.g. 99.999 and 99.9999 wt.% aluminum can beproduced in accordance with this invention on a highly consistent basis.That is, the equipment of the present invention can easily be scaled tosuitable production capacity at minimal costs.

Also, it will be noted that there are advantages in energy savings. Asnoted above, there is a large savings in energy required to operate theelectrolytic cell by virtue of the electrode placement. Another energysaving feature resides in recirculating one fraction of molten aluminumfrom the fractional crystallization step to the charging well of theelectrolytic cell. It should be noted that the recycling of the moltenaluminum shown in FIGS. 1, 4 and 5 is not necessarily via a directconduit, but may be via transport of crucibles of molten aluminum fromone stage to another. The important feature with respect to energysavings is that reheating and remelting between stages is not necessary(i.e. the reheating and remelting of room temperature aluminum).

The following example is still further illustrative of the invention.

EXAMPLE

Aluminum alloy was employed as starting material which contained about99.98 wt.% aluminum with the balance impurities as set forth in thetable under "Makeup Feed". This alloy was charged at a rate of 45.36 kgs(100 lbs/day) in solid form into the forewell of a Hoopes cellsubstantially as described in FIG. 2. The cell had been previously setup to have three molten layers. That is, an anode layer was provided inthe bottom of the cell and the density adjusted by the use of copper. Anelectrolytic layer consisted essentially of approximately 44 wt.% AlF₃,22 wt.% NaF, 18 wt.% BaF₂ and 16 wt.% CaF₂. The third layer comprisedessentially 99.993 wt.% aluminum. The cell was operated more or lesscontinuously at a current density of about 2 amps/in². An amount ofpurified aluminum consisting essentially of 99.993 wt.% aluminum wasremoved daily from the cell, the amount removed being substantiallycommensurate with the charging rate. The purified product had animpurity level as shown in the table under the heading "Hoopes Product".It should be noted that the total feed to the cell was 68.04 kgs (150lbs) of impure metal; that is, there was included in the feed 22.68 kgs(50 lbs) of metal recycled from the crystallization process. When therecycled metal was combined with the makeup feed, it provided a feed of99.91 wt.% aluminum, the impurity level being essentially as shown inthe table under the heading "Combined Feed".

Approximately 68.04 kgs (150 lbs) of the purified aluminum product fromthe Hoopes cell was charged to a fractional crystallization unitsubstantially as shown in FIG. 3. Heat was removed from the unit at themetal-air interface to induce crystallization until about 70% of thestarting material was crysallized. During the crystallization operation,the crystals formed were tamped. After the crystallization, molten metalhigh in impurity or mother liquor was drained off the crystal mass. Thecrystals remaining were subjected to remelting from top to bottom suchthat the molten metal from the top or surface layers of crystals washedthe bottommost layers. Remelting was carried out until approximately thelast 30% of the crystals were taken as the purified product. Productfrom this first crystallization was approximately 99.999 wt.% aluminum,the impurities being substantially as set forth in the table under theheading "Stage 1 Product".

The mother liquor or downgraded material was subjected to a secondfractional crystallization process to provide a purity comparable withthe product from the Hoopes cell. That is, about 45.35 kgs (100 lbs) ofdowngraded material from Stage 1 consisting of about 99.987 wt.%aluminum and impurities, as set forth in the table under the heading"Stage 1 Downgrade," was subjected to a second fractionalcrystallization, and 22.68 kgs (50 lbs) of the purified product ofapproximately 99.993% purity therefrom was blended with the product fromthe Hoopes cell to provide the feed for the Stage 1 fractionalcrystallization step. The mother liquor or downgraded materialconsisting of about one half of the total amount fed into Stage R andhaving a purity of about 99.98 wt.% aluminum, as shown in the tableunder the heading "Stage R Downgrade," was returned to be used as feedfor the Hoopes cell as indicated hereinabove.

                                      TABLE                                       __________________________________________________________________________                              Stage 1                                                                           Stage 1                                                                             Stage R                                                                            Stage R                              Makeup Feed                                                                              Combined Feed                                                                         Hoopes Prod.                                                                         Prod.                                                                             Downgrade                                                                           Prod.                                                                              Downgrade                            (ppm)      (ppm)   (ppm)  (ppm)                                                                             (ppm) (ppm)                                                                              (ppm)                                __________________________________________________________________________    Si  400    286     20     3   37    20   54                                   Fe  400    282     15     1   29    15   43                                   Cu  20     33      25     3.5 47    25   59                                   Mn  10     7       0.2    0.18                                                                              0.22  0.2  0.24                                 Mg  10     9       2.0    <0.5                                                                              3.5   2.0  5.0                                  Ni  10     10      3.0    <0.1                                                                              6.0   3.0  9.0                                  Zn  20     17      1.0    0.5 1.5   1.0  2.0                                  Ga  200    167     1.0    0.3 1.7   1.0  2.4                                  B   2      3       3.0    0.4 5.6   3.0  8.2                                  Cr  5      4       <0.1   <0.15                                                                             0     0    0                                    Ti  30     20      <0.1   <0.15                                                                             0     0    0                                    V   30     20      <0.1   <0.15                                                                             0     0    0                                    Zr  20     17      <0.1   <0.15                                                                             0     0    0                                    Total                                                                             1160   878     71     10  131   70   182                                  Purity                                                                            99.88  99.91   99.993 99.999                                                                            99.987                                                                              99.993                                                                             99.982                               (wt. %)                                                                       __________________________________________________________________________

Thus, it can be seen from the above example that neglecting transferlosses, almost 45.36 kgs (100 lbs) of 99.999 wt.% aluminum can beobtained for every 45.36 kgs (100 lbs) of impure aluminum charged to thesystem. Thus, by using two crystallization stages, 67% of the Hoopesproduct was recovered directly as 99.999 wt.% aluminum without thenecessity of recycling back through the Hoopes cell. This is significantsince it will be remembered that it is most desirable to minimize theamount of downgrade metal recycled to the Hoopes cell because, as notedearlier, purification using the Hoopes cell is several times moreexpensive than the fractional crystallization.

Furthermore, it will be noted from the table that the process enablessignificant lowering of all of the elements considered critical forcryogenic application, i.e. titanium, vanadium, zirconium, chromium,manganese and iron.

Having thus described the invention, what is claimed is:
 1. A highpurity mortar suitable for binding refractory brick, the mortar beingresistant to attack by molten aluminum and comprising:(a) 43 to 89 wt.%alumina; (b) 10 to 45 wt.% calcium aluminate cement; (c) 0.5 to 10 wt.%zinc borosilicate; and (d) 0.1 to 1.5 wt.% boric acid.
 2. The mortar inaccordance with claim 1 wherein the alumina is in the range of 54 to 74wt.%.
 3. The mortar in accordance with claim 1 wherein the calciumaluminate is in the range of 25 to 40 wt.%.
 4. The mortar in accordancewith claim 1 wherein the zinc borosilicate is in the range of 1.0 to 5.0wt.%.
 5. The mortar in accordance with claim 1 wherein the boric acid isin the range of 0.2 to 0.8 wt.%.
 6. A high purity mortar suitable forbinding refractory brick, the mortar being resistant to attack by moltenaluminum and comprising:(a) 54 to 74 wt.% alumina; (b) 25 to 40 wt.%calcium aluminate cement; (c) 1.0 to 5.0 wt.% zinc borosilicate; and (d)0.2 to 0.8 wt.% boric acid.
 7. The mortar in accordance with claim 1wherein the alumina has a size of not greater than 8 mesh (TylerSeries).